| 摘要: |
| 目的 解决某天然气净化厂三甘醇（TEG）脱水装置干净化气水露点及装置能耗偏高的问题。方法 采用现场实验和数值模拟的方法，深入探究了TEG脱水装置工艺参数优化与技术改进的方向。结果 ①排除了现场过滤器及再生系统等设备对TEG溶液的影响，干净化气水露点主要受湿净化气进装置温度、重沸器温度和贫液进吸收塔温度3种因素的影响，影响程度从大到小的顺序为：湿净化气进装置温度＞重沸器温度＞贫液进吸收塔温度；②TEG脱水装置能耗与重沸器温度、富液进再生塔温度和TEG循环量呈正相关关系，现场TEG脱水装置能耗主要受重沸器温度的控制；③在保证干净化气水露点在冬、春季≤-8 ℃、在夏、秋季≤0 ℃的前提下，建议夏、秋季采用湿净化气进装置温度为22.52 ℃、重沸器温度为164 ℃、贫液进吸收塔温度为49.24 ℃的工作模式，冬、春季采用湿净化气进装置温度为15.00 ℃、重沸器温度为168.98 ℃、贫液进吸收塔温度为41.57 ℃的工作模式。在该工作模式下，装置能耗分别降低42.60%和47.57%；④仅靠理论优化工艺参数不能满足实际应用的需求，建议提升湿净化气和TEG相关冷却设备的性能，降低湿净化气温度或TEG贫液温度的高温效果，以减少因过度使用高负荷重沸器所产生的成本问题。结论 通过采取上述措施，可降低干净化气水露点及装置能耗，为TEG脱水工艺的优化提供参考。 |
| 关键词: 天然气 脱水 三甘醇 正交试验 响应面法 降低能耗 |
| DOI：10.3969/j.issn.1007-3426.2025.03.006 |
| 分类号: |
| 基金项目: |
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| Process and energy consumption optimization of natural gas triethylene glycol dehydration unit |
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QIN Yang1, ZHAO Hongliang1, YANG Zhenghai1, LI Xiaolu1, XIE Shiyi2, JIN Xinxiu1,3
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1.PetroChina Changqing Oilfield Company, Xi'an, Shaanxi, China;2.PetroChina Southwest Oil & Gasfield Company, Chengdu, Sichuan, China;3.The University of New South Wales, Sydney, Australia
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| Abstract: |
| Objective The aim is to solve the problems of high water dew point of dry purified gas and high energy consumption of triethylene glycol (TEG) dehydration unit in a natural gas purification plant. Method Field experiments and numerical simulation methods were used to deeply explore the optimization and technical improvement directions of TEG dehydration unit process parameters. Result Firstly, the influences of on-site filters, regeneration system and other equipment on the TEG solution were excluded. The water dew point of dry purified gas was mainly affected by three factors: the temperature of wet purified gas into the unit, the temperature of reboiler and the temperature of lean liquid into the absorber. The order of influence degree from large to small was: the temperature of wet purified gas into the unit ＞ the temperature of reboiler ＞ the temperature of lean liquid into the absorber. Secondly, the energy consumption of the TEG dehydration unit was positively correlated with the reboiler temperature, the temperature of the rich liquid into the regenerator and the TEG circulation volume. The energy consumption of the on-site TEG dehydration unit was mainly controlled by the reboiler temperature. Thirdly, on the premise of ensuring that the purified gas water dew point in winter and spring was not higher than -8 ℃ and in summer and autumn not higher than 0 ℃, respectively, it was recommended to adopt the working mode of wet purified gas into the unit temperature of 22.52 ℃, reboiler temperature of 164 ℃ and lean liquid into the absorber temperature of 49.24 ℃ in summer and autumn, and the working mode of wet purified gas into the unit temperature of 15.00 ℃, reboiler temperature of 168.98 ℃ and lean liquid into the absorber temperature of 41.57 ℃ in winter and spring. Under this working mode, the energy consumption of the unit was reduced by 42.60% and 47.57%, respectively. Fourthly, Relying only on theoretical optimization of process parameters could not meet the needs of practical applications. It was recommended that the performance of cooling equipment for both wet purified gas and TEG should be improved. This would help reduce the high temperature effects of wet purified gas and TEG lean liquid, thereby minimizing the cost issues associated with excessive use of high-load reboilers. Conclusion By implementing the above measures, the water dew point of dry purified gas and the energy consumption of the unit can be reduced, which can provide a reference for the optimization of the TEG dehydration process. |
| Key words: natural gas dehydration triethylene glycol orthogonal experiment response surface method reducing energy consumption |
